Process of manufacturing gasoline



Aug. 9, 1938. J. R. ROSE PROCESS OF MANUFACTURING GASOLINE Filed Nov. 19, 1956 n n HIIIIH .n hll||||| f In. U

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ATTORNEYS PatentedV Aug, A9,1938 l. L

James B. Rose, Edgeworth,

three-fourths to Michael L. `Joseph C. l'recs, Pittsburgh, Pa.

PROCESS F TENT] OFFICE Application November 19, 193s, seria No. 111,654:

. t v 1 claim. This inventionrelates to a process of extracting gasoline from the gases resulting from the cracking'of oil in the manufacture ot "gasoline, i

andhas for its general object to ,obtain a maximum recovery of gasoline from such gases and to accomplish such recovery inV an economical and eilicient manner.

The gases resulting from the cracking of oil in the manufacture of gasoline are known to the trade as "still gases, "receiver gasesf and sta-f bilizer gases, and contain unsaturates varying in richness (such-as acetylene, propylene, butylene, etc.) and varying in proportions, according to the grades or theoils cracked. l5 For convenience of description, the gases treated will be referred to in the claims as still gases. Hitherto these gases have been allowed to go to waste, except as to such relatively small proportions of the same as may have been employed 0 in the heating of the various units in the cracking plants. vBy virtue of my invention, I am enabled to reconstruct'these gases by the treatment set forth hereinafter, thereby to produce gasoline therefrom on a commercial basis; that is, on a 25 basis which will yield a high proportion of gasoline at low cost.`

My process will he described in connection with the drawing, whichv shows a diagrammatic or schematic representation ol an apparatus whereby it may he realized.

The mixture of gases resulting from the craching oi the oil, hereinafter designated still gases,

is delivered through a suitable pipe l into a gas holder t, under a pressure'slightly above `that-ol 35 the atmosphere. From this holder, the gases are conducted to a compressor 3, where they are subjected to a pressure ci from 200 lbs. to 1500 lbs.

per square inch and are delivered under this pressure into a suitable heating stove t, where the l temperature is raised from 200 F. to 1500? F.

' The mixture of gases is then conducted, while still under the pressure noted, through one or more catalyst chambers 5 and are delivered thence to a cooler 6, which effects a partial condensation the gases so treated `into liquid form, this condensation into liquid form having been facilitated by the two preceding steps which cooperate to .dissociate the unsaturates and recombine 50 the dissociated constituents thereof into gasoline.

the limits stated hereinbefore in accordance with the proportions oi heavier unsaturates in the particular gaseous mixture which is to Abe treated and in accordance with the character of the cata- 55 lyst to which they are subjected, it being a matter 'I'he pressures and temperatures vary between (Cl. ISB-10) of common knowledge' that the temperatures toy which a catalyst must be heated in order to insure a suitable reaction and the pressures to which gases must be subjected in order to pass them through a catalyst will vary with the particular catalyst employed. Y

The liquid condensed from the gases and whatever gases may have been uncondensed' are conducted through a pressure-reducing valve 'i into a receiver 8, wherein further non-condensable o gases will pass out through the top ofthe receiver into a pipe 9. The gasesin this pipe may be deliveredin whole or inpart either to the atmos phere or into the pipe I through the pipe- I l, by suitable manipulation of the pressure regulating valves il and i i". The gases delivered from the receiver into the pipes i0 and i will be collected in the holder 2 for the purpose of being recycled, together with the incoming waste gases from the cracking operation. The pressure reducing "valve 1, which is located at the outlet from the cooler, serves to reduce any pressures which may exist in the cooler and in the catalyst chambersto approximately 150 lbs. per square inch, and this pressure, being necessary for the stabilization oi the product, is maintained in the subsequent steps of my process.

Byrecycling'the gases, a further separation is accomplished as to the unsaturates that may not havebeen reconstructed and condensed in their hrst run through the process.

The liquid (gasoline) inthe bottom of the receiver is delivered hy means ol a charging pump ll and a. pipe it into a stabilizing tower it, lor thepurpose of stabilizing the product underthe pressure noted and of effecting, by means of a condenser it, a further condensation of such gases as may have been separated from the product. From the condenser what are known as dry gases may be delivered through the pipe it and the automatic regulator valve il to the stills for use in the heating operations.

By raising the temperature to 1000" to 1500 F., a considerable quantity of the saturates are broken down, as well astheunsaturates, and are thereafter cooled and condensed and pumped into the stabilizing tower, as explained hereinbeiore, where they are reboiled in order to separate the heavier from the lighter ends.

A 4catalyst which I have found particularly 4eiiicient in the realization of my process is one made from ground phosphate rock, mixed preferably in equal proportions by weight with what is known to the trade as "re bond (a mixture oi silica sand and water glass). This mixture of phosphate rock and lire bond is then thoroughly mixed with water, and is then dried and broken into lumps. While the proportions specied hereinbefore for the phosphate rock and nre bond in the catalyst will result in a product which-has given satisfactory results at temperatures of approximately 800 F., these proportions may be varied to accommodate variations in the particular unsaturates and mixtures thereof which are treated.

Having thus described my invention, what I claim is: u

The process ot manufacturing gasoline from stlllgases which consists in heating said gases to a temperature between 800 and 1500 F. and

under a pressure of from 200 lbs. to 1500 lbs. per square inch; passing the gases thus heated and while`under the said pressure in contact with a catalyst comprising a dried mixture in substantially equal proportions by weight of phosphate rock and re bond; cooling the gases while under the said pressure therehyto ei'Iect a preliminary separation of condensable products; reducing the pressure on the said gases and condensable products and delivering them into a receiving chamber; recycling gases evolved in said chamber; and stabilizing the condensable products under superatmospheric pressure. 

